WO2001027027A1 - Procede et dispositif permettant de reduire les rejets d'ammoniac dans les applications comprenant l'elimination de nox par un procede scr et/ou sncr - Google Patents

Procede et dispositif permettant de reduire les rejets d'ammoniac dans les applications comprenant l'elimination de nox par un procede scr et/ou sncr Download PDF

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Publication number
WO2001027027A1
WO2001027027A1 PCT/US2000/027948 US0027948W WO0127027A1 WO 2001027027 A1 WO2001027027 A1 WO 2001027027A1 US 0027948 W US0027948 W US 0027948W WO 0127027 A1 WO0127027 A1 WO 0127027A1
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WO
WIPO (PCT)
Prior art keywords
flue gas
adsorbent
specified
ammonia
passing
Prior art date
Application number
PCT/US2000/027948
Other languages
English (en)
Inventor
Felix E. Spokoyny
Original Assignee
Hera, Llc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hera, Llc filed Critical Hera, Llc
Priority to AU17511/01A priority Critical patent/AU1751101A/en
Publication of WO2001027027A1 publication Critical patent/WO2001027027A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/79—Injecting reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/54—Nitrogen compounds
    • B01D53/56—Nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/90—Injecting reactants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/003—Arrangements of devices for treating smoke or fumes for supplying chemicals to fumes, e.g. using injection devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L15/00—Heating of air supplied for combustion
    • F23L15/04—Arrangements of recuperators
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D19/00—Regenerative heat-exchange apparatus in which the intermediate heat-transfer medium or body is moved successively into contact with each heat-exchange medium
    • F28D19/04—Regenerative heat-exchange apparatus in which the intermediate heat-transfer medium or body is moved successively into contact with each heat-exchange medium using rigid bodies, e.g. mounted on a movable carrier
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/10—Nitrogen; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/20—Sulfur; Compounds thereof
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • a method and apparatus for reducing the amount of unused ammonia ("ammonia slip") in instances where ammonia is provided to SNCR and/or SCR processes for reducing NOx pollution in flue gas produced by a fossil fuel burning facility incorporates a regenerative heat exchanger (i.e. an air preheater) for absorbing heat on the flue gas side, and releasing such absorbed heat to heat the incoming combustion air.
  • the invention herein includes absorbent/desorbent media carried by at least some of the heat transfer elements of the heat exchanger. The media is active to adsorb at least a portion of the ammonia slip before the flue gas stream is exhausted to the environment, and to desorb essentially an equilibrium portion of such adsorbed ammonia into the incoming combustion air.
  • the invention relates generally to the reduction of nitrogen oxides from flue gas, and, more particularly, to a method and apparatus for reducing ammonia slip to the atmosphere through adsorption/desorption at the air preheater, while simultaneously relieving the air heater pluggage due to ammonia sulfate and bisulfate formation and, farther, to reduce the amount of ammonia attaching to the flyash collected by precipitators or baghouses.
  • Much of the electrical power used in homes and businesses throughout the world is produced in power plants that burn a fossil fuel (i.e. coal, oil, or gas) in a boiler.
  • a fossil fuel i.e. coal, oil, or gas
  • the resulting hot exhaust gas (also sometimes termed "flue gas") turns a gas turbine or boils water to produce steam, which turns a steam turbine, and the turbine cooperates with a generator to produce electrical power.
  • the flue gas stream is passed through an air preheater, such as a rotating wheel heat exchanger, that transfers heat from the flue gas to an incoming air stream, that thereafter flows to the combustor.
  • the partially cooled flue gas is directed from the air preheater to the exhaust stack.
  • NOx nitrogen oxides
  • SOx sulfur oxides
  • fly ash is often removed by an electrostatic precipitator (ESP) and/or a baghouse.
  • the invention herein deals with those particular pollution control systems which utilize ammonia within the process in order to initiate, cause and/or supplement the removal of NOx, and in particular SCR, SNCR and/or staged systems (i.e. systems which include one or more SCR or SNCR systems).
  • SCR sulfur-driven chemical vapor deposition
  • SNCR SNCR
  • staged systems i.e. systems which include one or more SCR or SNCR systems.
  • a nitrogenous compound such as ammonia
  • the ammonia reacts with the NOx to form nitrogen and water, reducing the NOx content of the flue gas.
  • the reaction of ammonia and NOx may be performed at high temperature without a catalyst, a process termed “selective non-catalytic reduction” (SNCR), or at lower temperature in the presence of a catalyst, a process termed “selective catalytic reduction” (SCR).
  • SNCR selective non-catalytic reduction
  • SCR selective catalytic reduction
  • SNCR is accomplished by injecting a nitrogenous compound, such as a source of ammonia, into the hot flue gas, and permitting the reduction reaction to occur in the flue gas.
  • a nitrogenous compound such as a source of ammonia
  • U.S. Patent Nos. 3,900,554, 4,208,386, and 4,325,924 illustrate known types of SNCR applications. SCR is generally accomplished at lower temperatures than SNCR, and necessitates the use of a catalyst, which is placed onto surfaces of catalyst modules, which are positioned within a flue gas stream.
  • U.S. Patent No. 5,104,629 illustrates one known type of SCR installations.
  • the flyash may not be able to be sold, and the utility will have to pay for the disposal.
  • ammonia slip i.e. larger SCR units, more responsive control arrangements, early replacement of catalyst, and the like
  • ammonia slip will indeed enter the air preheater. It is specifically to the ammonia slip which enters the air preheater for which the instant invention is directed.
  • the present invention overcomes, or in the least, greatly alleviates the prior art deficiencies discussed above, in an efficient, cost effective and novel manner.
  • the present invention includes an adsorbent compound which is integrally formed with, or adhered to, the exposed surfaces of some of the air preheater heating elements.
  • the adsorbent is selected and structured to act as a molecular sieve to adsorb, or capture, molecular ammonia on the gas side of the air preheater, and to desorb, or release, such captured ammonia on the air side of the preheater.
  • the desorbed ammonia is either destroyed in the boiler fire ball or, in the alternative, is used to destroy NOx in an SNCR and/or SCR stage of the NOx reduction system.
  • the preferred pore size of the adsorbent material will be sufficient to adsorb ammonia (i.e 2.8 A), but less than 4A, so as to prevent SO 2 or SO 3 penetration.
  • other critical criteria for the application of the existing invention is the selection of preheater layers or partial layers on which elements having adsorbent surfaces will be positioned, as well as the minimum catalytic activity of such adsorbent (i.e. to alleviate the concern for amplifying the potential of ammonium sulfate/bisulfate problems, or creating additional SO 3 where perhaps none is required).
  • an object and advantage of the present invention is to provide a method and apparatus for alleviating the problems of ammonia slip to the environment, by including a means and method for adsorbing excess system ammonia at the gas side of the air preheater and continually releasing an equilibrium portion of such adsorbed ammonia as the heating elements rotate to the air side of the preheater.
  • FIG. 1 is a schematic view of a portion of a power plant flue gas flow system according to the invention
  • FIG. 2 is a exemplary schematic view of heating elements illustrating a single element from the hot end layer, intermediate layer, and cold end layer of a heat exchanger, showing the distribution of adsorbent materials thereon.
  • FIG. 1 schematically illustrates a fossil fuel burning power plant 10 which utilizes an adsorption/desorption system 12 of the present invention therewithin.
  • a carbonaceous fael such as coal is combusted with air in a furnace 20 and produces, in addition to power, combustion products contained within the flue gas.
  • the flue gas may contain nitrogen oxides (NOx), fly ash, SO 2 , SO 3 , and other undesirable pollutants.
  • the plant 10 includes an SNCR system 14 for reducing NOx within the furnace 20, and an SCR systeml ⁇ for reducing NOx downstream from the furnace.
  • the combustion flue gas exits from the furnace 20 into an exhaust duct assembly 22.
  • the exhaust duct assembly 22 extends from the furnace 20 through a known air preheater 24, typically of the rotary regenerative type.
  • the air preheater 24 is provided to absorb heat on the gas side, and use such absorbed heat to heat incoming air on the air side of the preheater 24.
  • the combustion air is provided by blower 27, and is directed to the furnace 20 through the inlet duct assembly 26.
  • the flue gas passes from the preheater 24, through a suitable cleaning device, such as a baghouse or, as shown, an electrostatic precipitator, schematically illustrated as 28, and is exhausted from the power plant 10 through a stack 30.
  • the discussion of the power plant 10 is intended to be highly schematic in nature, and it is not deemed necessary to provide more information and background to understand, practice and enable the present invention.
  • the present invention is compatible with such other systems and may, wherever applicable, be used with them.
  • the level or amount of nitrogen oxides in the flue gas is an important consideration because of present day standards, which severely limit NOx emissions from many fossil fuel burning power generation facilities.
  • regulations may require the usage of an SNCR system 14, an SCR system 16, or, on occasion, a combination SNCR/SCR system (a staged system, such as is shown in Fig. 1).
  • SNCR and/or SCR systems 14 and 16, respectively are well established, and detailed descriptions thereof are not necessary to one skilled in the art to understand the need for and operation of the instant invention.
  • the particular schematically illustrated SCR system 16 is of the type which is for limited NOx reduction, the present invention is also compatible with for the more conventional full scale systems commonly used for 90% + reduction.
  • a nitrogenous compound such as urea, in the case of SNCR 14, or ammonia, in the case of SCR 16 is injected into the flue gas stream to convert NOx into free nitrogen and water.
  • urea in the case of SNCR 14
  • ammonia in the case of SCR 16
  • ammonia slip This excess ammonia is commonly known as "ammonia slip" and, as will be described hereinafter, can result in several problems at the air preheater 44, and downstream thereof. It is particularly to ammonia slip entering the air preheater 24 to which the instant invention is directed.
  • the air preheater 24 includes a plurality of heating elements 46, which are heated by the passage of the hot flue gas.
  • the elements 46 are positioned, in a known manner, within baskets, or partitions, positioned within the wheel 47 of the preheater 24.
  • wheel 47 rotatably carries two or more levels of elements 46.
  • the wheel 47 of the heat exchanger 24 continuously rotates about its axis 49, which may be oriented either vertically or horizontally, to carry the exchange elements 46 from the flue gas side 42 to an air side 48. During such rotation, the heat in the heating elements 46 is transferred to a flow of cool incoming air being provided from blower 27.
  • Fig. 2 schematically illustrates hot end heat exchange element 46(a), intermediate elements 46 (b) and cold end elements 46 (c), from layers 50, 52 and 54, respectively.
  • the heat exchange elements 46 are coated with an adsorbent.
  • the coated elements 46 shown as elements 46 (a) and 46 (b) in the embodiment illustrated, carry a suitable adsorbent (shown as shaded) on the exposed surfaces thereof.
  • the intermediate element 46(b) is illustrated as having absorbent on only one half the height thereof, as exemplary of conditions which are indicative of not applying adsorbent to the entire height. Other conditions may require all or none of element having adsorbent being applied thereto.
  • the adsorbent which is preferably selected and applied to specific surfaces in accordance with the guidelines discussed below, is operable to adsorb ammonia slip from the flue gas passing thereby, and to desorb an equilibrium portion of the adsorbed ammonia to the combustion air passing thereby as the wheel 47 rotates from the flue gas side 42 to the air side 48.
  • preferred adsorbent is zeolite,, carbon, or a combination of zeolite and carbon.
  • Zeolite is presently the preferred adsorbent. Further, because consistency and uniform pore size is necessary, it is anticipated that a manufactured, rather than a natural zeolite will be preferred in most instances. In this regard, a range of contemplated pore size diameter is 2.8 to 3.8 A for the zeolite is recommended, with a preferred size of approximately 3.0 A. Note, the lower end of the above range is selected because ammonia gas, which is to be adsorbed, has a molecular size of 2.8 A, and the upper range is selected because SO 2 and SO 3 , have a molecular size of more than 4.0 A.
  • the adsorbent should be substantially catalytically inactive in the temperature zone in which it will operate. The primary reason for this is that any catalytic activity will increase the conversion of SO 2 to SO 3 , which in most instances is not a desirable effect.
  • the typical temperature of flue gas passing through an air preheater 24 ranges from up to 700°F at the hot end to 250°F at the cold end.
  • typical catalytic activity threasholds for a V-Ti oxide catalyst is 550 to 750°F.
  • the adsorbent should be applied to elements 46 between the following limits (along the depth of preheater 24):
  • T mm is the low limit defined by the temperature of formation of ammonium sulfate/bisulfate and their deposition on ash particle surfaces. This temperature is a function of SO 3 and NH 3 concentrations in the flue gas.
  • T m3X is the high limit defined by the condition that maximum adsorption capability of the adsorbent for adsorbate partial pressure on the "gas" side and maximum “metal" temperature at this longitudinal location is not less than the maximum adsorption capability for adsorbate partial pressure on the "air” side and rninimum “metal” temperature at the same longitudinal location.
  • the calculated temperature range in most instances, will be 750°F to 300°F, with a preference of 650°F to 450°F.
  • adsorbent Another governing factor concerning the placement of adsorbent is that the surface area to which adsorbent is applied, and the amount of adsorbent, should provide a maximum adsorption capability of the adsorbent exposed to the flue gas at any moment at operating adsorbent temperature and the partial pressure of the ammonia in the flue gas, which should be significantly higher ( i.e. at least an order of magnitude higher) than the amount of ammonia that should be removed from the gas stream during the time period when an individual adsorbent element is exposed to flue gas.
  • the adsorbing layer should be specifically structured to create a molecular sieve with a consistent selected diameter.
  • the length (depth) of the adsorbing material should be preferably longer than the distance traveled by the concentration wave of the adsorbate in the longitudinal direction during the time of adsorbent exposure to the flue gas to avoid a breakthrough of ammonia to a cooler zone of the air preheater 24, even through a small angular portion of the gas side sectors.
  • the adsorbent should preferably be hydrophobic and water resistant to allow for cleaning of the air preheater 42 by water washing and also to withstand the occurrence of occasional tube leaks.
  • the adsorbent will be selected from a group of materials whose specific storage capacity for ammonia in the operating temperature and partial pressure range is more sensitive to pressure variations than to temperature variations.
  • the adsorbing material should be applied to those layers of the preheater 24 where the effect of the "metal" temperature swing on the specific storage capacity for ammonia is overcompensated by the effect of ammonia partial pressure swing.
  • the adsorbing material should preferably be selected from a group of adsorbents efficient in the temperature range of 300 - 700°F, and partial pressure of ammonia of 10 "6 - 3x10 "5 bar.
  • alternative adsorbent substrates are anticipated, such as a honeycomb structure; depending upon conditions, perhaps only the hot end or intermediate layer of the elements 46 will be coated with an adsorbent compound, or perhaps only part of the hot end or intermediate layer elements will be coated; if deemed appropriate to reduce the metal temperature swing, and increase the ammonia transfer potential, it may be desirable to consider increasing the heat capacity of the heating element carrying adsorbent, by increasing it thickness; and the like. Accordingly, the invention is not to be limited except as by the appended claims.

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  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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  • Treating Waste Gases (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Abstract

L'invention concerne un procédé et un dispositif permettant de réduire la quantité d'ammoniac non utilisé (rejets d'ammoniac), lors d'un apport d'ammoniac destiné à des procédés de réduction catalytique non sélective (SNCR) et/ou de réduction catalytique sélective (SCR), destinés à réduire la pollution due au NOX dans les fumées émises par une installation (10) de combustion utilisant des combustibles fossiles. Une telle installation (10) comprend un échangeur (24) de chaleur régénératif tel qu'un réchauffeur d'air, lequel absorbe la chaleur du côté (42) des gaz de combustion, et libère la chaleur ainsi absorbée pour chauffer l'air de combustion entrant. L'invention concerne comprend un milieu d'absorption/désorption supporté par au moins une partie des éléments (46) de transfert thermique de l'échangeur (24) de chaleur. Ce milieu agit par absorption d'au moins une partie de l'excédent d'ammoniac avant que le flux de gaz de combustion soit évacué dans l'environnement, et par désorption d'une quantité sensiblement équivalente d'ammoniac ainsi absorbé dans l'air de combustion entrant.
PCT/US2000/027948 1999-10-12 2000-10-10 Procede et dispositif permettant de reduire les rejets d'ammoniac dans les applications comprenant l'elimination de nox par un procede scr et/ou sncr WO2001027027A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU17511/01A AU1751101A (en) 1999-10-12 2000-10-10 Method and apparatus for reducing "ammonia slip" in scr and/or sncr nox removal applications

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US09/416,665 1999-10-12
US09/416,665 US6264905B1 (en) 1999-10-12 1999-10-12 Method and apparatus for reducing “ammonia slip” in SCR and/or SNCR NOX removal applications

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WO2001027027A1 true WO2001027027A1 (fr) 2001-04-19

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CN103657411A (zh) * 2013-12-13 2014-03-26 哈尔滨锅炉厂有限责任公司 用于scr烟气脱硝系统的旋流混合装置
CN103776026A (zh) * 2014-01-24 2014-05-07 东南大学 一种利用烟气余热降低电站锅炉高温腐蚀的装置及方法
JP6026614B1 (ja) * 2015-09-29 2016-11-16 株式会社プランテック ごみ焼却炉排ガス処理設備
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CN111189062A (zh) * 2020-03-03 2020-05-22 南京科远智慧科技集团股份有限公司 一种监测脱硝氨逃逸对下游回转式空气预热器影响的方法

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